CN108586296B - Continuous synthesis method of p-nitrotoluene-o-sulfonic acid - Google Patents
Continuous synthesis method of p-nitrotoluene-o-sulfonic acid Download PDFInfo
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- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/02—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof
- C07C303/04—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof by substitution of hydrogen atoms by sulfo or halosulfonyl groups
- C07C303/06—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof by substitution of hydrogen atoms by sulfo or halosulfonyl groups by reaction with sulfuric acid or sulfur trioxide
Abstract
A continuous process for synthesizing p-nitrotoluene-o-sulfonic acid includes such steps as melting p-nitrotoluene, dissolving in organic solvent or inorganic solvent, introducing the mixture of p-nitrotoluene and sulfur trioxide into membrane sulfonating reactor for sulfonating reaction, filtering the liquid reaction product containing inorganic solvent to remove solvent, ageing, directly introducing the liquid reaction product containing no solvent or organic solvent into ageing tank, stirring and ageing. Adding deionized water for hydrolysis after aging is finished, wherein a hydrolysis product without an organic solvent is p-nitrotoluene-o-sulfonic acid; adding deionized water to extract the hydrolysate containing the organic solvent, and dissolving the hydrolysate in a water phase to obtain the p-nitrotoluene-o-sulfonic acid. The invention has the advantages of low production cost, no waste acid, high safety performance and continuous production.
Description
Technical Field
The invention relates to a continuous synthesis method of p-nitrotoluene-o-sulfonic acid.
Background
P-nitrotoluene-o-sulfonic acid, also known as 4-nitrotoluene-2-sulfonic acid, is abbreviated as NTS acid and has CAS registry number 121-03-9. As a very important dye intermediate, the main applications are as follows: 1) oxidizing to obtain 4,4 '-dinitrostilbene-2, 2' -disulfonic acid (DNS acid), and reducing to obtain 4,4 '-diaminostilbene-2, 2' -disulfonic acid (DSD acid) or 4-amino-4 '-nitrostilbene-2, 2' -disulfonic acid (ANSD acid); 2) a series of mono-triazole stilbene fluorescent whitening agents are synthesized as raw materials.
At present, the synthesis process route of p-nitrotoluene-o-sulfonic acid at home and abroad is to use p-nitrotoluene as a raw material and to sulfonate the p-nitrotoluene by sulfonating agents such as fuming sulfuric acid, chlorosulfonic acid or sulfur trioxide. For example, patent CN 1762992a discloses a method for recycling sulfuric acid filtrate, which comprises adding 20% oleum as sulfonating agent into molten p-nitrotoluene for sulfonation, crystallizing and filtering the reaction product, mixing the collected sulfuric acid filtrate with the molten p-nitrotoluene, reacting with 50-65% oleum as sulfonating agent, and recycling the sulfuric acid filtrate. Compared with the existing industrial production method, the method has the advantages that a large amount of waste sulfuric acid with the concentration of 55-60% is not generated, and the generated sulfuric acid can be recycled. However, it is not considered that SO is consumed per molecule as the reaction proceeds3Molecular water is generated, sulfuric acid in the system is gradually diluted, waste sulfuric acid is continuously generated, and accumulated waste sulfuric acid still becomes a burden of enterprises in industrial production with fixed yield. Secondly, 50-65% of fuming sulfuric acid used for production belongs to extremely unstable and highly corrosive national control dangerous chemicals, is usually solid under cold conditions, is difficult to store and has high transportation cost. In addition, the production is carried out in a reaction kettle, the reaction using fuming sulfuric acid needs uninterrupted stirring, a large amount of energy is consumed, a large amount of time is wasted, and discharging is needed after the reaction of each kettle is finished, so that continuous production cannot be realized. Therefore, the existing sulfuric acid sulfonation and fuming sulfuric acid sulfonation cannot meet the requirement of large-scale production no matter considering economic cost and environmental protection pressure.
Disclosure of Invention
The invention aims to provide a continuous synthesis method of p-nitrotoluene-o-sulfonic acid, which has the advantages of low production cost, no waste acid, high safety performance and continuous production.
The method takes gas sulfur trioxide as a sulfonating agent, p-nitrotoluene is sulfonated in a membrane reactor, and the p-nitrotoluene ortho-sulfonic acid without waste sulfuric acid is obtained after gas-liquid separation and post-treatment.
The invention relates to a continuous synthesis method of p-nitrotoluene-o-sulfonic acid, which is characterized by comprising the following steps:
(1) melting paranitrotoluene, or dissolving the paranitrotoluene in an organic solvent or an inorganic solvent, and simultaneously introducing mixed gas with the temperature of 45-90 ℃ and the volume concentration of sulfur trioxide of 3-30% into a membrane sulfonation reactor with the length of 2-8m, wherein the molar ratio of the paranitrotoluene to the sulfur trioxide is 1.0: 0.9-1.3, carrying out sulfonation reaction at 60-110 ℃, then carrying out gas-liquid separation, and emptying the gas after passing through a demister;
(2) filtering the liquid reaction product containing inorganic solvent to remove the solvent, then feeding the liquid reaction product into an aging tank, directly feeding the liquid reaction product containing no solvent or organic solvent into the aging tank, and stirring and aging at 75-140 ℃ for 10-90 min;
(3) transferring the mixture into a hydrolysis tank after aging, adding deionized water, stirring and hydrolyzing at 60-140 ℃ for 10-90min, wherein a hydrolysis product without an organic solvent is p-nitrotoluene-o-sulfonic acid;
(4) adding deionized water into hydrolysate containing organic solvent for extraction, and dissolving in water phase to obtain water solution product of p-nitrotoluene-o-sulfonic acid;
(5) and filtering the separated inorganic solvent or extracting the separated organic solvent for recycling.
In the method, the organic solvent for dissolving the paranitrotoluene is one of chloroform, dichloroethane, dioxane, o-dichlorobenzene, m-dichlorobenzene, p-dichlorobenzene, hexane, heptane and octane; the inorganic solvent for dissolving the paranitrotoluene is concentrated sulfuric acid or thionyl chloride.
In the above method, the molar ratio of the p-nitrotoluene to the organic solvent or inorganic solvent is 1: 0.5-5.
In the method, the source of the sulfur trioxide is obtained by catalyzing sulfur dioxide with a catalyst.
In the method, the diluent gas in the sulfur trioxide mixed gas is dry air with a dew point lower than minus 50 ℃, and the temperature of the diluent gas is 45-90 ℃.
In the method, the adding amount of water in the hydrolysis reaction in the step (3) is 0.2-5.0% of the mass of the p-nitrotoluene-o-sulfonic acid.
In the method, the usage amount of the deionized water in the extraction process of the step (4) is 1-4 times of the mass of the p-nitrotoluene-o-sulfonic acid.
The invention provides a preparation method of p-nitrotoluene ortho-sulfonic acid, which has the advantages of low production cost, no waste acid, high safety performance and continuous production. The method has the advantages that the occupied area of reaction equipment is small, the equipment is not corroded in the production process, the mass transfer and heat transfer efficiency of the used membrane sulfonation reactor is high, the product conversion rate is high, the number of byproducts is small, and the yield of the target product is higher than 95 wt%; when the solvent is not used, less equipment is needed, the post-treatment is simple, and the production cost is lower; when the solvent is used, the fluidity of the reaction system can be increased, the mass transfer and the heat transfer of the reaction system are further promoted, the obtained product has better quality, the solvent can be recycled, no waste is generated, and the method is green and environment-friendly and has very important application value.
Detailed Description
Example 1
Introducing para-nitrotoluene in a 65 ℃ molten state at a rate of 68.6g/min and 5% sulfur trioxide mixed gas with a volume concentration of 45 ℃ at a rate of 248L/min, namely, simultaneously introducing the para-nitrotoluene and the 45 ℃ sulfur trioxide mixed gas into a 2.5 m long falling film type sulfonation reactor according to a molar ratio of 1:0.95, wherein the diluent gas in the sulfur trioxide mixed gas is dry air with a dew point lower than-50 ℃, and adjusting the temperature of cooling water of a jacket of the film type reactor to control the reaction temperature to be 70 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. After 30min, the reactant enters an aging tank to be stirred and aged for 20min at 80 ℃, then enters a hydrolysis tank, is added with 16g of water and stirred and hydrolyzed for 20min at 70 ℃, and the obtained product is the p-nitrotoluene-o-sulfonic acid, and the content of the p-nitrotoluene-o-sulfonic acid is measured to be 96.9 wt%.
Example 2
Introducing 80 ℃ molten p-nitrotoluene and 70 ℃ sulfur trioxide mixed gas with volume concentration of 15% into a 3.0 m long falling film type sulfonation reactor at a speed of 68.6g/min and a speed of 103L/min, namely according to a molar ratio of 1:1.1, wherein the diluent gas in the sulfur trioxide mixed gas is dry air with a dew point lower than-50 ℃, and adjusting the temperature of cooling water of a jacket of the film type reactor to control the reaction temperature to be 90 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. After 30min, the reactant enters an aging tank to be stirred and aged for 60min at 100 ℃, then enters a hydrolysis tank, 65g of water is added, and then the mixture is stirred and hydrolyzed for 60min at 100 ℃, so that the obtained product is the p-nitrotoluene-o-sulfonic acid, and the content of the p-nitrotoluene-o-sulfonic acid is determined to be 98.1 wt%.
Example 3
Introducing p-nitrotoluene in a molten state at 100 ℃ and 30% sulfur trioxide mixed gas at 90 ℃ into a 6.0 m long falling film sulfonation reactor at a rate of 68.6g/min and a rate of 65L/min, namely according to a molar ratio of 1:1.3, wherein the diluent gas in the sulfur trioxide mixed gas is dry air with a dew point lower than-50 ℃, and adjusting the temperature of cooling water of a jacket of the film reactor to control the reaction temperature to be 110 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. After 30min, the reactant enters an aging tank to be stirred and aged for 90min at the temperature of 130 ℃, then enters a hydrolysis tank, 130g of water is added, and then the mixture is stirred and hydrolyzed for 90min at the temperature of 120 ℃, so that the obtained product is the p-nitrotoluene-o-sulfonic acid, and the content of the p-nitrotoluene-o-sulfonic acid is measured to be 97.6 wt%.
Example 4
2742.8g of p-nitrotoluene and 1000g of 98% sulfuric acid mixed solution in a molten state at the temperature of 60 ℃ and mixed gas of 10% sulfur trioxide at the volume concentration of 60 ℃ are simultaneously introduced into a falling film type sulfonation reactor with the length of 3.5 m at the speed of 93.1g/min and the speed of 178L/min, namely according to the molar ratio of 1:1.3, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film type reactor is adjusted to control the reaction temperature to be 110 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. The reactant is cooled and filtered, enters an aging tank, is stirred and aged for 30min at 90 ℃, then enters a hydrolysis tank, is added with 43 g of water, is stirred and hydrolyzed for 30min at 80 ℃, and the obtained product is the p-nitrotoluene-o-sulfonic acid, and the content of the p-nitrotoluene-o-sulfonic acid is measured to be 96.5 wt%.
Example 5
2742.8g of p-nitrotoluene and 2379.4g of thionyl chloride mixed solution in a molten state at 70 ℃ are introduced into a falling film type sulfonation reactor with the length of 4.5 m at the speed of 128.1g/min and the speed of 80L/min of mixed gas of sulfur trioxide with the volume concentration of 20% at 50 ℃, namely according to the molar ratio of 1:1.2, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film type reactor is adjusted to control the reaction temperature to be 100 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. The reactant is cooled and filtered, enters an aging tank, is stirred and aged for 40min at 110 ℃, then enters a hydrolysis tank, is added with 65g of water, is stirred and hydrolyzed for 40min at 110 ℃, and the obtained product is the p-nitrotoluene-o-sulfonic acid, and the content of the p-nitrotoluene-o-sulfonic acid is measured to be 96.3 wt%.
Example 6
2742.8g of p-nitrotoluene and 3958.8g of dichloroethane mixed solution in a molten state at 75 ℃ is fed into a falling film sulfonation reactor which is 5.5m long at the speed of 167.6g/min and the speed of 66L/min of mixed gas of sulfur trioxide with the volume concentration of 25 percent at 75 ℃, namely according to the molar ratio of 1:1.15, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film reactor is adjusted to control the reaction temperature to be 75 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. Stirring and aging the reaction system at 120 ℃ for 50min, then feeding the reaction system into a hydrolysis tank, adding 130g of water, stirring and hydrolyzing the reaction system at 120 ℃ for 50min, adding 4344g of water into the reaction product for extraction, layering to obtain a water phase, namely, a p-nitrotoluene-o-sulfonic acid aqueous solution, and determining the content of the water phase to be 97.6 wt%.
Example 7
2742.8g of p-nitrotoluene and 8820g of o-dichlorobenzene mixed solution in a melting state at 85 ℃ is introduced into a falling film type sulfonation reactor with the length of 5.0m at the speed of 252.4g/min and the speed of 190L/min of mixed gas of sulfur trioxide with the volume concentration of 8 percent at 80 ℃, namely according to the molar ratio of 1:1.05, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film type reactor is adjusted to control the reaction temperature to be 85 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. Stirring and aging the reaction system at 105 ℃ for 70min, then entering a hydrolysis tank, adding 108g of water, stirring and hydrolyzing at 105 ℃ for 70min, adding 8688g of water into the reactant for extraction, and obtaining a water phase after layering, namely a p-nitrotoluene-o-sulfonic acid water solution, wherein the content of the water phase is determined to be 98.7 wt%.
Example 8
2742.8g of p-nitrotoluene and 6012g of heptane mixed liquid in a molten state at 95 ℃ is introduced into a falling film type sulfonation reactor with the length of 6.5m at the speed of 218.9g/min and the speed of 135L/min of mixed gas of sulfur trioxide with the volume concentration of 12% at 85 ℃, namely according to the molar ratio of 1:1.1, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film type reactor is adjusted to control the reaction temperature to be 105 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. The reaction system is stirred and aged for 80min at 95 ℃, then enters a hydrolysis tank, is stirred and hydrolyzed for 50min at 95 ℃ after 152 g of water is added, 13032g of water is added into the reactant for extraction, the water phase obtained after delamination is the water solution of p-nitrotoluene-o-sulfonic acid, and the content is determined to be 98.5 wt%.
Example 9
2742.8g of p-nitrotoluene and 8811g of dioxane mixed solution in a molten state at the temperature of 80 ℃ and mixed gas of 18 percent of sulfur trioxide at the volume concentration of 60 ℃ are simultaneously introduced into a falling film type sulfonation reactor with the length of 7.0m at the speed of 288.9g/min and the speed of 95L/min according to the molar ratio of 1:1.25, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film type reactor is adjusted to control the reaction temperature to be 75 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. Stirring and aging the reaction system at 75 ℃ for 50min, then entering a hydrolysis tank, adding 195g of water, stirring and hydrolyzing at 75 ℃ for 50min, adding 17376g of water into the reactant, extracting, layering to obtain a water phase, namely a p-nitrotoluene-o-sulfonic acid water solution, and determining the content to be 95.9 wt%.
Example 10
2742.8g of p-nitrotoluene and 8820g of m-dichlorobenzene mixed solution in a molten state at 100 ℃ is introduced into a falling film type sulfonation reactor 8.0m long at the speed of 252.4g/min and the speed of 190L/min of mixed gas of sulfur trioxide with the volume concentration of 8 percent at 80 ℃, namely according to the molar ratio of 1:1.05, wherein the diluent gas in the mixed gas of sulfur trioxide is dry air with the dew point lower than-50 ℃, and the temperature of cooling water of a jacket of the film type reactor is adjusted to control the reaction temperature to be 75 ℃. After gas-liquid separation, the tail gas is exhausted after passing through a demister. Stirring and aging the reaction system at 75 ℃ for 50min, then feeding the reaction system into a hydrolysis tank, adding 215g of water, stirring and hydrolyzing the reaction system at 75 ℃ for 50min, adding 15204g of water into the reaction product for extraction, layering to obtain a water phase, namely a p-nitrotoluene-o-sulfonic acid aqueous solution, and determining the content of the water phase to be 98.1 wt%.
Claims (5)
1. A continuous synthesis method of p-nitrotoluene-o-sulfonic acid is characterized by comprising the following steps:
(1) melting paranitrotoluene, or dissolving the paranitrotoluene in an organic solvent or an inorganic solvent, and simultaneously introducing mixed gas with the temperature of 45-90 ℃ and the volume concentration of sulfur trioxide of 3-30% into a membrane sulfonation reactor with the length of 2-8m, wherein the molar ratio of the paranitrotoluene to the sulfur trioxide is 1.0: 0.9-1.3, carrying out sulfonation reaction at 60-110 ℃, then carrying out gas-liquid separation, and emptying the gas after passing through a demister;
the organic solvent used for dissolving the paranitrotoluene is one of chloroform, dichloroethane, dioxane, o-dichlorobenzene, m-dichlorobenzene, paradichlorobenzene, hexane, heptane and octane;
the inorganic solvent for dissolving the paranitrotoluene is concentrated sulfuric acid or thionyl chloride;
(2) filtering the liquid reaction product containing inorganic solvent to remove the solvent, then feeding the liquid reaction product into an aging tank, directly feeding the liquid reaction product containing no solvent or organic solvent into the aging tank, and stirring and aging at 75-140 ℃ for 10-90 min;
(3) transferring the mixture into a hydrolysis tank after aging, adding deionized water, stirring and hydrolyzing at 60-140 ℃ for 10-90min, wherein a hydrolysis product without an organic solvent is p-nitrotoluene-o-sulfonic acid;
(4) adding deionized water into hydrolysate containing organic solvent for extraction, and dissolving in water phase to obtain water solution product of p-nitrotoluene-o-sulfonic acid;
(5) and filtering the separated inorganic solvent or extracting the separated organic solvent for recycling.
2. The continuous synthesis method of p-nitrotoluene-o-sulfonic acid as claimed in claim 1, wherein the molar ratio of p-nitrotoluene to organic solvent or inorganic solvent is 1: 0.5-5.
3. The continuous synthesis method of p-nitrotoluene-o-sulfonic acid as claimed in claim 1, wherein the diluent gas in the sulfur trioxide mixed gas is dry air with dew point lower than-50 ℃, and the temperature of the diluent gas is 45-90 ℃.
4. The continuous synthesis method of p-nitrotoluene o-sulfonic acid as claimed in claim 1, wherein the amount of water added in the hydrolysis reaction in step (3) is 0.2-5.0% by mass of p-nitrotoluene o-sulfonic acid.
5. The continuous synthesis method of p-nitrotoluene o-sulfonic acid as claimed in claim 1, wherein the amount of deionized water used in the extraction process of step (4) is 1-4 times of the mass of p-nitrotoluene o-sulfonic acid.
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| CN111302316B (en) * | 2020-03-05 | 2023-01-31 | 中国日用化学研究院有限公司 | Method and device for continuously preparing sulfamic acid |
| CN112694422B (en) * | 2021-01-14 | 2023-01-31 | 中国日用化学研究院有限公司 | Green continuous preparation method and device for joint production of dinonyl naphthalene disulfonic acid and alkyl benzene sulfonic acid |
| CN114031525B (en) * | 2021-11-10 | 2023-07-28 | 武汉青江化工黄冈有限公司 | Method for continuously preparing p-nitrotoluene ortho-sulfonic acid by using dynamic tubular reactor |
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